Catalyst for Conversion of Hydrocarbons, Process of Making and Process of Using Thereof - Incorporation-1

ABSTRACT

This invention is for a catalyst for conversion of hydrocarbons. The catalyst contains a zeolite having germanium and at least one selected from the group consisting of tin and boron incorporated into the zeolite framework and at least one metal selected from Group 10 deposited on the zeolite. The catalyst is prepared by synthesizing a zeolite having germanium and at least one selected from the group consisting of tin and boron incorporated into the zeolite framework; depositing the metal; and calcining after preparation of the zeolite and before or after depositing the metal. The catalyst may be used in a process for the conversion of hydrocarbons, such as propane to aromatics, by contacting the catalyst with alkanes having 2 to 12 carbon atoms per molecule and recovering the product.

BACKGROUND OF THE INVENTION

1. Field of the Invention

This invention relates to a catalyst for hydrocarbon conversion, e.g., acatalyst for the aromatization of alkanes, olefins and mixtures thereofhaving two to twelve carbon atoms per molecule. The catalyst is amicroporous silicate, aluminosilicate, aluminophosphate orsilicoaluminophosphate on which a metal has been deposited.

2. Description of the Prior Art

Crystalline silicates, aluminosilicates, aluminophosphates andsilicoaluminophosphates are known catalysts for hydrocarbon conversionand may contain other metals. An aluminosilicate such as zeolite mayinclude not only aluminum and silicon but other trivalent elements whichreplace aluminum and other tetravalent elements which replace silicon.Also, other elements may be deposited on the silicate, aluminosilicate,aluminophosphate or silicoaluminophosphate.

U.S. Pat. No. 4,310,440 discloses crystalline aluminophosphates having aframework structure with chemical composition in mole ratios of 1Al₂O₃:1.0±0.2 P₂O₅ and being microporous with uniform pores of nominaldiameters from about 3 to about 10 angstroms.

U.S. Pat. No. 4,440,871 discloses crystalline microporoussilicoaluminophosphates having pores which are uniform and have nominaldiameters of greater than about 3 angstroms with a chemical compositionof mole fractions of silicon, aluminum and phosphorus within thepentagonal composition area defined by

Mole Fraction x y z A 0.01 0.47 0.52 B 0.94 0.01 0.05 C 0.98 0.01 0.01 D0.39 0.60 0.01 E 0.01 0.60 0.39where x, y and z are the mole fractions of silicon, aluminum andphosphorus and ACBDE are points defining a pentagonal area of a ternarydiagram as shown in FIG. 1 of U.S. Pat. No. 4,440,871.

SUMMARY OF THE INVENTION

This invention provides a catalyst containing silicon, aluminum,phosphorus, as needed to form a silicate, aluminosilicate,aluminophosphate (AlPO) or silicoaluminophosphate (SAPO) with at leastone other element selected from Group 4, Group 5, Group 13, Group 14,Group 15 and the first series transition metals in a three dimensionalinterconnecting crystalline tetrahedral framework. The crystallinetetrahedral framework is synthesized from an aqueous gel containing, asneeded, a silica source, an aluminum source, a phosphorus source, asource for the Group 4, Group 5, Group 13, Group 14, Group 15 and thefirst series transition metal element(s) and, optionally, an organicstructure-directing agent. The reaction mixture is heated to formcrystals and then cooled. The crystals are separated from the synthesisliquor and are washed, dried and calcined. At least one metal selectedfrom Group 6, Group 7, Group 8, Group 9 or Group 10 is deposited on thesilicate, aluminosilicate, aluminophosphate or silicoaluminophosphate(hereinafter referred to as “deposited metal”). The catalyst may be usedin a process for converting C₂-C₁₂ hydrocarbons into aromatics.

One example of the invention is a catalyst on which at least one Group10 metal, such as platinum, is deposited on a zeolite having at leasttwo elements selected from Group 13 or Group 14, such as germanium andeither tin or boron, in the zeolite framework. This example includes aprocess for synthesizing a zeolite by: a) preparing a zeolite having atleast two elements selected from Group 13 or Group 14, such as germaniumand either tin or boron, in the zeolite framework; b) depositing atleast one metal selected from Group 10 on the zeolite; and c) calciningthe zeolite, said calcining occurring after preparation of the zeolite,before depositing at least one metal selected from Group 10 on thezeolite or after depositing at least one metal selected from Group 10 onthe zeolite. This example of the invention also includes a process forthe conversion of hydrocarbons of: a) contacting a hydrocarbon streamcontaining alkanes, olefins and mixtures thereof having 2 to 12 carbonatoms per molecule with at least one zeolite-based catalyst wherein thezeolite has at least two elements selected from Group 13 or Group 14,such as germanium and either tin or boron, in the zeolite framework andwherein at least one metal selected from Group 10 has been deposited onthe zeolite; and b) recovering the product. Another example of theinvention is a catalyst on which at least one Group 10 metal, such asplatinum, is deposited on a zeolite having at least one element selectedfrom Group 13 or Group 14, such as boron, in the zeolite framework. Thisexample includes a process for synthesizing a zeolite by: a) preparing azeolite having boron incorporated into the zeolite framework; b)depositing at least one metal selected from Group 10 on the zeolite; andc) calcining the zeolite on which at least one metal selected from Group10 is deposited, said calcining occurring after preparation of thezeolite, before depositing at least one metal selected from Group 10 onthe zeolite or after depositing at least one metal selected from Group10 on the zeolite. This example of the invention also includes a processfor the conversion of hydrocarbons of contacting a hydrocarbon streamcontaining alkanes, olefins and mixtures thereof having 2 to 12 carbonatoms per molecule with at least one zeolite-based catalyst whereinboron is incorporated into the zeolite framework and wherein at leastone metal selected from Group 10 has been deposited on the zeolite andrecovering the product.

Another example of the invention is a ZSM-5 zeolite having germanium andat least one selected from the group consisting of tin and boronincorporated into the zeolite framework. This example also includes aprocess for synthesizing a zeolite by preparing a ZSM-5 zeolitecontaining germanium and at least one selected from the group consistingof tin and boron incorporated into the zeolite framework and calciningthe zeolite.

DETAILED DESCRIPTION OF THE INVENTION

Crystalline silicates, aluminosilicates, aluminophosphates andsilicoaluminophosphates have uniform pores through which molecules candiffuse. Aluminosilicates include zeolites. Examples of zeolites are MFI(ZSM-5), BEA (Beta), MWW (MCM-22), MOR (Mordenite), LTL (Zeolite L), MTT(ZSM-23), MTW (ZSM-12), TON (ZSM-22) and MEL (ZSM-11).

Crystalline silicates, aluminosilicates, aluminophosphates andsilicoaluminophosphates have structures of TO₄ tetrahedra, which form athree dimensional network by sharing oxygen atoms where T representstetravalent elements, such as silicon; trivalent elements, such asaluminum; and pentavalent elements, such as phosphorus. “Zeolite” in thepresent application includes aluminosilicates with openthree-dimensional framework structures composed of corner-sharing TO₄tetrahedra, where T is Al or Si, but also includes tetravalent,trivalent and divalent T atoms which able to isoelectronically replaceSi and Al in the framework, e.g., germanium(4+), titanium (4+), boron(3+), gallium (3+), iron (3+), zinc (2+) and beryllium (2+). “Zeolite”is primarily a description of structure, not composition.

Silicates, aluminosilicates, aluminophosphates andsilicoaluminophosphates generally crystallize from an aqueous solution.The typical technique for synthesizing silicates, aluminosilicates,aluminophosphates or silicoaluminophosphates comprises converting anaqueous gel of a silica source, an aluminum source and a phosphorussource, as needed, to crystals by a hydrothermal process, employing adissolution/recrystallization mechanism. The reaction medium may alsocontain an organic structure-directing agent which is incorporated inthe microporous space of the crystalline network during crystallization,thus controlling the construction of the network and assisting tostabilize the structure through the interactions with the silicon,aluminum or phosphorus components.

The aqueous gel contains in addition to the silica source, the aluminumsource, the phosphorus source, as needed, and the optional organicstructure-directing agent, and a source of at least one other elementfrom Group 4, Group 5, Group 13, Group 14, Group 15 or the first seriestransition metals to be incorporated into the framework of the silicate,aluminosilicate, aluminophosphate or silicoaluminophosphate.

Examples of the silica source are silicon oxide or silica (SiO₂) whichis available in various forms, such as silica sol, commerciallyavailable as Ludox AS-40™, precipitated silica, commercially availableas Ultrasil VN3SP™ and fumed silica, commercially available as Aerosil200™.

Examples of the aluminum source are sodium aluminate, aluminum nitrate,aluminum sulfate, aluminum hydroxide and pseudobohemite.

Examples of the phosphorus source are phosphoric acid (85 wt %), P₂0₅,orthophosphoric acid, triethylphosphate and sodium metaphosphate.

Examples of the source of Group 4, Group 5, Group 13, Group 14, Group 15and the first series transition metals are oxides, chlorides, sulfates,alkoxides, fluorides, nitrates and oxalates.

Examples of the structure-directing agent are organic amine andquaternary ammonium compounds and salts and cations thereof, such astetra n-propyl ammonium hydroxide, tetra n-propyl ammonium bromide andtetra n-propyl ammonium chloride, tetraethyl ammonium hydroxide,hexamethyleneimine, 1,4-di(1′4′-diazabicyclo[2.2.2]octane)butanehydroxide, morpholine, cyclohexylamine and diethylethanolamine,N,N′-diisopropyl imidazolium cation, tetrabutylammonium compounds,di-n-propylamine (DPA), tripropylamine, triethylamine (TEA),triethanolamine, piperidine, 2-methylpyridine, N,N-dimethylbenzylamine,N,N-diethylethanolamine, dicyclohexylamine, N,N-dimethylethanolamine,choline cation, N,N′-dimethylpiperazine, 1,4-diazabicyclo(2,2,2)octane,N′,N′,N,N-tetramethyl-(1,6)hexanediamine, N-methyldiethanolamine,N-methyl-ethanolamine, N-methyl piperidine, 3-methyl-piperidine,N-methylcyclohexylamine, 3-methylpyridine, 4-methyl-pyridine,quinuclidine, N,N′-dimethyl-1,4-diazabicyclo(2,2,2) octane ion;di-n-butylamine, neopentylamine, di-n-pentylamine, isopropylamine,t-butyl-amine, ethylenediamine, pyrrolidine, 2-imidazolidone, aN-benzyl-1,4-diazabicyclo[2.2.2]octane cation, a1-[1-(4-chlorophenyl)-cyclopropylmethyl]-1-ethyl-pyrrolidinium or1-ethyl-1-(1-phenyl-cyclopropylmethyl)-pyrrolidium cation and mixturesthereof.

The reaction may also utilize an acid as a reagent. The acid may be aBronsted acid or a Lewis acid. Examples without limitation of an aciduseful in the present invention are sulfuric acid, acetic acid, nitricacid, phosphoric acid, hydrochloric acid, hydrofluoric acid, oxalic acidor formic acid.

The reaction mixture is stirred and heated to a temperature of about100° C. to about 200° C. to form crystals. The reaction mixture iscooled to room temperature. The crystals are separated from thesynthesis liquor. The liquid portion of the synthesis liquor may beremoved by filtration, evaporation, spray drying or any other means forremoving liquid, e.g., water, from the crystals. The crystals are washedwith water and then dried and calcined.

The silicates are essentially aluminum-free but may contain aluminum andother impurities up to 500 ppm.

The aluminosilicates may have a silicon to aluminum atomic ratio (Si:Al)greater than 2:1. In one embodiment of the present invention, thesilicon to aluminum atomic ratio is in the range from 15:1 to 200:1. Inanother embodiment of the present invention, the silicon to aluminumatomic ratio is in the range from 18:1 to 100:1.

The aluminophosphates may have an aluminum to phosphorus atomic ratio(Al:P) in the range from about 0.8:1 to about 1.2:1 as disclosed in U.S.Pat. No. 4,310,440, hereby incorporated by reference.

The silicoaluminophosphates may have a silicon to aluminum to phosphorusatomic ratio represented by (S_(x)Al_(y)P_(z))O₂ where “x”, “y” and “z”represent the mole fractions of silicon, aluminum and phosphorusrespectively, present as tetrahedral oxides, said mole fractions beingsuch that they are within the pentagonal compositional area defined bypoints ABCD and E of a ternary diagram with values represented in thetable below:

Mole Fraction x y z A 0.01 0.47 0.52 B 0.94 0.01 0.05 C 0.98 0.01 0.01 D0.39 0.60 0.01 E 0.01 0.60 0.39as disclosed in U.S. Pat. No. 4,440,871, hereby incorporated byreference.

The amount of Group 4, Group 5, Group 13, Group 14, Group 15 and thefirst series transition metals present in the crystalline framework isin the range from 0.1 wt. % to 25 wt. %. In one embodiment of thepresent invention, this range is from 0.1 wt. % to 10 wt. %. In anotherembodiment of the present invention, this range is from 0.1 wt. % to 5wt. %.

The silicate, aluminosilicate, aluminophosphate orsilicoaluminophosphate has average pore size in the range from 2angstroms to 20 angstroms, i.e., microporous.

At least one metal selected from Group 6, Group 7, Group 8, Group 9 orGroup 10 is deposited on the silicate, aluminosilicate, aluminophosphateor silicoaluminophosphate (“deposited metal”). The metal is depositednot only on the surface of the silicate, aluminosilicate,aluminophosphate or silicoaluminophosphate but also in the pores andchannels which occur in the silicate, aluminosilicate, aluminophosphateor silicoaluminophosphate. The metal is deposited on the silicate,aluminosilicate, aluminophosphate or silicoaluminophosphate by any knownmethod of depositing a metal on a silicate, aluminosilicate,aluminophosphate or silicoaluminophosphate. Typical methods ofdepositing a metal on a silicate, aluminosilicate, aluminophosphate orsilicoaluminophosphate are ion exchange, impregnation and vapordeposition. In one embodiment of the present invention, the metal ispresent in the range from 0.05% to 3% by weight. In another embodimentof the present invention, the metal is present in the range from 0.1% to2% by weight. In another embodiment of the present invention, the metalis present in the range from 0.2 to 1.5% by weight.

However, for silicate, aluminosilicate, aluminophosphate orsilicoaluminophosphate-based catalysts on which metals have beendeposited, the process temperatures and catalyst regenerationtemperatures cause the metal to “sinter”, i.e., agglomeration of themetal particles resulting in an increase of metal particle size on thesurface of the zeolite and a decrease of metal surface area, causing aloss of catalyst performance, specifically catalyst performance, e.g.,activity and/or selectivity.

Without the present invention and its claims being limited by theory, itis believed that certain elements in the framework and certain metalsdeposited on the silicate, aluminosilicate, aluminophosphate orsilicoaluminophosphate associate to resist sintering of the depositedmetal. U.S. Pat. No. 6,784,333 discloses and claims analuminum-silicon-germanium zeolite on which platinum has been depositedfor use in a process for the aromatization of hydrocarbons. The presenceof germanium in the framework of the zeolite and the presence ofplatinum deposited on the zeolite apparently results in higherselectivity for benzene, toluene and xylenes (BTX) which remainsessentially constant over a significant time on stream. Without theinvention of U.S. Pat. No. 6,784,333 and its claims being limited bytheory, it may be that the germanium in the framework and the platinumdeposited on the zeolite associate such that the platinum remainsdispersed and sintering is reduced.

Besides germanium, there may be other elements in the crystallineframework which associate with platinum or other deposited metals.Elements in the crystalline framework may be selected from Group 4,Group 5, Group 13, Group 14, Group 15 and the first series transitionmetals of the Periodic Table of Elements. Specific examples of theseelements are germanium, boron, gallium, indium, tin, titanium,zirconium, vanadium, chromium, iron, niobium and phosphorus. One or moreelements may be in the crystalline framework. Specific examples ofelements in the framework are germanium and at least one selected fromthe group consisting of tin and boron.

Besides platinum, there may be other deposited metals which associatewith germanium or other elements in the crystalline framework. Depositedmetals may be selected from Group 6, Group 7, Group 8, Group 9 and Group10 of the Periodic Table of Elements. Specific examples of the depositedmetal are platinum, molybdenum, rhenium, nickel, ruthenium, rhodium,palladium, osmium and iridium. One or more metals, such as bimetallics,e.g., Pt/Sn, Pt/Ge, Pt/Pb or metal/metal oxide combinations, e.g.Pt/GeO₂, may be deposited.

The crystalline framework of which these elements from Group 4, Group 5,Group 13, Group 14, Group 15 and the first series transition metals arepart and on which metals selected from Group 6, Group 7, Group 8, Group9 and Group 10 are deposited need not be limited to a zeolite but may beany microporous silicate, aluminosilicate, aluminophosphate orsilicoaluminophosphate.

Before or after deposition of the metal, the silicate, aluminosilicate,aluminophosphate or silicoaluminophosphate may be bound by oxides orphosphates of magnesium, aluminum, titanium, zirconium, thorium,silicon, boron or mixtures thereof. The process steps of binding anddepositing metal can occur in any order. Binding may occur before orafter metal deposition.

The catalyst may be calcined at different stages in the synthesis. Forexample, there may be a first calcination of the silicate,aluminosilicate, aluminophosphate or silicoaluminophosphate to removethe organic structure-directing agent followed by metal deposition andsubsequent calcinations at lower temperatures. The calcination to removethe organic structure-directing agent is at a temperature of about 300°C. to about 1000° C. or about 300° C. to about 750° C. for a timesufficient to remove essentially all of any structure-directing agent,e.g., one to six hours or about four hours. One example of calcinationis at 550° C. for ten hours. Calcination may occur after binding. Thiscalcination is at a temperature in the range of from about 300° C. toabout 1000° C. for a time in the range of from about one hour to about24 hours. Calcination may also occur after metal deposition to fix themetal. This calcination should not exceed a temperature of 500° C. andmay be at a temperature of about 200° C. to about 500° C. for a time inthe range of from about 0.5 hour to about 24 hours. These calcinationsneed not be separate but may be combined to accomplish more than onepurpose. When the silicate, aluminosilicate, aluminophosphate orsilicoaluminophosphate is calcined, it may be bound or unbound and itmay have metal deposited on it or not. Calcination can occur in anenvironment of oxygen, nitrogen, hydrogen, water vapor, helium andmixtures thereof.

The catalyst, bound and unbound, will have porosity in addition to theuniform porosity of the silicate, aluminosilicate, aluminophosphate orsilicoaluminophosphate. For an unbound catalyst, the average pore sizeof the catalyst can vary for bound and unbound catalyst and is in therange from 2 angstroms to 100 angstroms. In one embodiment of thepresent invention, the average pore size is in the range from 5angstroms to 50 angstroms. In another embodiment of the presentinvention, the average pore size is in the microporous range from 5angstroms to 20 angstroms. For a bound catalyst, the average pore sizeof the catalyst may vary from 5 angstroms up to 100 microns.

Some catalysts used for hydrocarbon conversion are susceptible to sulfurpoisoning. However, for some catalysts used for hydrocarbon conversion,modest amounts of sulfur, such as about 0 to 200 ppm in the feed, areacceptable and sometimes preferred. The catalyst may also be pretreatedwith sulfur. A standard sulfurization method that is well known in theart consists in heating in the presence of a sulfur compound, such ashydrogen sulfide, or a mixture of a sulfur compound and an inert gas,such as hydrogen or nitrogen, to a temperature of between 150 and 800°C. Non-limiting examples of sulfur compounds are H₂S, an organosulfidecompound, such as dimethyl disulfide or DMSO (dimethyl sulfoxide), orC_(n)H_(2n+2)S or C_(n)H_(2n+2)S₂, where n=1-20. In one embodiment ofthe present invention, the temperature is between 250 and 600° C.

The catalyst may contain a reaction product, such as a sulfide of thedeposited metal, that is formed by contacting the catalyst with sulfuror a sulfur compound. In one embodiment of the present invention, theamount of sulfur on the catalyst is in the range of from 10 ppm to 0.1wt. %.

The catalyst may also contain elements other than sulfur, such as tin,germanium or lead. These elements would be present in the range of from1:1 to 1:100 as a ratio of the deposited metal to tin, germanium orlead. These elements may be added to the catalyst by wet impregnation,chemical vapor deposition or other methods known in the art.

The silicate, aluminosilicate, aluminophosphate orsilicoaluminophosphate-based catalyst which contains at least oneelement selected from Group 4, Group 5, Group 13, Group 14, Group 15 andthe first series transition metals isomorphously incorporated into thezeolite framework and at least one metal selected from Group 6, Group 7,Group 8, Group 9 and Group 10 deposited on the zeolite can be used in aprocess for conversion of hydrocarbon streams containing C₂-C₁₂ alkanes,olefins or mixture thereof which may be straight, branched, cyclic ormixtures thereof, into aromatics.

The zeolite may be base-exchanged with an alkali metal or alkaline earthmetal, such as cesium, potassium, sodium, rubidium, barium, calcium,magnesium and mixtures thereof, to reduce acidity and form a non-acidiczeolite. A non-acidic zeolite has substantially all of its cationicsites of exchange, e.g., those typically associated with aluminum,occupied by nonhydrogen cationic species, e.g., alkali or alkaline earthmetals. These cationic sites are often responsible for cracking ofhydrocarbons into undesired products. A zeolite may be non-acidic byexchange with a base or by having a low aluminum content. Thebase-exchange may occur before or after the noble metal is deposited.Such a base-exchanged catalyst may be used to convert C₆-C₁₂ alkanes,such as might be obtained from natural gas condensate, light naphtha,raffinate from aromatics extraction and other refinery or chemicalprocesses, to aromatics, such as benzene, ethyl benzene, toluene andxylenes. Base-exchange may take place during synthesis of the zeolitewith an alkali metal or alkaline earth metal being added as a componentof the reaction mixture or may take place with a crystalline zeolitebefore or after deposition of the noble metal. The zeolite isbase-exchanged to the extent that most or all of the cations associatedwith aluminum are alkali metal or alkaline earth metal. An example of amonovalent base:aluminum molar ratio in the zeolite after base exchangeis at least about 0.9. For a divalent or trivalent base, the molar ratiowould be half (0.45) or a third (0.3) as that for a monovalent base,respectively, and for mixtures of monovalent, divalent and trivalentbases, the above molar ratios would be apportioned by their respectivecontent in the mixture.

Depending on the element incorporated into the zeolite framework, thezeolite may be non-acidic without base-exchange, e.g., boron, germaniumor tin in an aluminum-free zeolite. “Aluminum-free” has a meaning ofhaving aluminum content of no more than 0.4 wt %.

Examples of hydrocarbon conversion processes for which this catalyst canbe used are:

(A) The catalytic cracking of a naphtha feed to produce light olefins.Typical reaction conditions include from about 500° C. to about 750° C.,pressures of subatmospheric or atmospheric, generally ranging up toabout 10 atmospheres (gauge) and catalyst residence time (volume of thecatalyst/feed rate) from about 10 milliseconds to about 10 seconds.(B) The catalytic cracking of high molecular weight hydrocarbons tolower weight hydrocarbons. Typical reaction conditions for catalyticcracking include temperatures of from about 400° C. to about 700° C.,pressures of from about 0.1 atmosphere (bar) to about 30 atmospheres,and weight hourly space velocities of from about 0.1 to about 100 hr⁻¹.(C) The transalkylation of aromatic hydrocarbons in the presence ofpolyalkylaromatic hydrocarbons. Typical reaction conditions include atemperature of from about 200° C. to about 500° C., a pressure of fromabout atmospheric to about 200 atmospheres, a weight hourly spacevelocity of from about 1 to about 100 hr⁻¹ and an aromatichydrocarbon/polyalkylaromatic hydrocarbon mole ratio of from about 1/1to about 16/1.(D) The isomerization of aromatic (e.g., xylene) feedstock components.Typical reaction conditions for such include a temperature of from about230° C. to about 510° C., a pressure of from about 0.5 atmospheres toabout 50 atmospheres, a weight hourly space velocity of from about 0.1to about 200 hr⁻¹ and a hydrogen/hydrocarbon mole ratio of from about 0to about 100.(E) The dewaxing of hydrocarbons by selectively removing straight chainparaffins. The reaction conditions are dependent in large measure on thefeed used and upon the desired pour point. Typical reaction conditionsinclude a temperature between about 200° C. and 450° C., a pressure upto 3,000 psig and a liquid hourly space velocity from 0.1 to 20 hr⁻¹.(F) The alkylation of aromatic hydrocarbons, e.g., benzene andalkylbenzenes, in the presence of an alkylating agent, e.g., olefins,formaldehyde, alkyl halides and alcohols having 1 to about 20 carbonatoms. Typical reaction conditions include a temperature of from about100° C. to about 500° C., a pressure of from about atmospheric to about200 atmospheres, a weight hourly space velocity of from about 1 hr⁻¹ toabout 100 hr⁻¹ and an aromatic hydrocarbon/alkylating agent mole ratioof from about 1/11 to about 20/1.(G) The alkylation of aromatic hydrocarbons, e.g., benzene, with longchain olefins, e.g., C₁₄ olefin. Typical reaction conditions include atemperature of from about 50° C. to about 200° C., a pressure of fromabout atmospheric to about 200 atmospheres, a weight hourly spacevelocity of from about 2 hr⁻¹ to about 2000 hr⁻¹ and an aromatichydrocarbon/olefin mole ratio of from about 1/1 to about 20/1. Theresulting products from the reaction are long chain alkyl aromaticswhich when subsequently sulfonated have particular application assynthetic detergents.(H) The alkylation of aromatic hydrocarbons with light olefins toprovide short chain alkyl aromatic compounds, e.g., the alkylation ofbenzene with propylene to provide cumene. Typical reaction conditionsinclude a temperature of from about 10° C. to about 200° C., a pressureof from about 1 to about 30 atmospheres, and an aromatic hydrocarbonweight hourly space velocity (WHSV) of from 1 hr⁻¹ to about 50 hr⁻¹.(I) The hydrocracking of heavy petroleum feedstocks, cyclic stocks, andother hydrocrack charge stocks. The zeolite-bound high silica zeolitewill contain an effective amount of at least one hydrogenation componentof the type employed in hydrocracking catalysts.(J) The alkylation of a reformate containing substantial quantities ofbenzene and toluene with fuel gas containing short chain olefins (e.g.,ethylene and propylene) to produce mono- and dialkylates. Preferredreaction conditions include temperatures from about 100° C. to about250° C., a pressure of from about 100 to about 800 psig, a WHSV-olefinfrom about 0.4 hr⁻¹ to about 0.8 hr¹, a WHSV-reformate of from about 1hr⁻¹ to about 2 hr⁻¹ and, optionally, a gas recycle from about 1.5 to2.5 vol/vol fuel gas feed.(K) The alkylation of aromatic hydrocarbons, e.g., benzene, toluene,xylene, and naphthalene, with long chain olefins, e.g., C₁₄ olefin, toproduce alkylated aromatic lube base stocks. Typical reaction conditionsinclude temperatures from about 100° C. to about 400° C. and pressuresfrom about 50 to 450 psig.(L) The alkylation of phenols with olefins or equivalent alcohols toprovide long chain alkyl phenols. Typical reaction conditions includetemperatures from about 100° C. to about 250° C., pressures from about 1to 300 psig and total WHSV of from about 2 hr⁻¹ to about 10 hr⁻¹.(M) The conversion of light paraffins to olefins and/or aromatics.Typical reaction conditions include temperatures from about 425° C. toabout 760° C. and pressures from about 10 to about 2000 psig.(N) The conversion of light olefins to gasoline, distillate and luberange hydrocarbons. Typical reaction conditions include temperatures offrom about 175° C. to about 500° C. and a pressure of from about 10 toabout 2000 psig.(O) Two-stage hydrocracking for upgrading hydrocarbon streams havinginitial boiling points above about 200° C. to premium distillate andgasoline boiling range products or as feed to further fuels or chemicalsprocessing steps. The first stage can be the zeolite-bound high silicazeolite comprising one or more catalytically active substances, e.g., aGroup 8 metal, and the effluent from the first stage would be reacted ina second stage using a second zeolite, e.g., zeolite Beta, comprisingone or more catalytically active substances, e.g., a Group 8 metal, asthe catalyst. Typical reaction conditions include temperatures fromabout 315° C. to about 455° C., a pressure from about 400 to about 2500psig, hydrogen circulation of from about 1000 to about 10,000 SCF/bbland a liquid hourly space velocity (LHSV) of from about 0.1 to 10 hr⁻¹.(P) A combination hydrocracking/dewaxing process in the presence of thezeolite-bound high silica zeolite comprising a hydrogenation componentand a zeolite such as zeolite Beta. Typical reaction conditions includetemperatures from about 350° C. to about 400° C., pressures from about1400 to about 1500 psig, LHSV from about 0.4 to about 0.6 hr⁻¹ and ahydrogen circulation from about 3000 to about 5000 SCF/bbl.(Q) The reaction of alcohols with olefins to provide mixed ethers, e.g.,the reaction of methanol with isobutene and/or isopentene to providemethyl-t-butyl ether (MTBE) and/or t-amyl methyl ether (TAME). Typicalconversion conditions include temperatures from about 20° C. to about200° C., pressures from 2 to about 200 atm, WHSV (gram-olefin per hourper gram-zeolite) from about 0.1 hr⁻¹ to about 200 hr⁻¹ and an alcoholto olefin molar feed ratio from about 0.1/1 to about 5/1.(R) The disproportionation of aromatics, e.g. the disproportionation oftoluene to make benzene and xylenes. Typical reaction conditions includea temperature of from about 200° C. to about 760° C., a pressure of fromabout atmospheric to about 60 atmosphere (bar), and a WHSV of from about0.1 hr⁻¹ to about 30 hr⁻¹.(S) The conversion of naphtha (e.g., C₆-C₁₀) and similar mixtures tohighly aromatic mixtures. Thus, normal and slightly branched chainedhydrocarbons, preferably having a boiling range above about 40° C., andless than about 200° C., can be converted to products having asubstantially higher octane aromatics content by contacting thehydrocarbon feed with the zeolite at a temperature in the range of fromabout 400° C. to 600° C., preferably 480° C. to 550° C. at pressuresranging from atmospheric to 40 bar, and liquid hourly space velocities(LHSV) ranging from 0.1 to 15 hr⁻¹.(T) The adsorption of alkyl aromatic compounds for the purpose ofseparating various isomers of the compounds.(U) The conversion of oxygenates, e.g., alcohols, such as methanol, orethers, such as dimethylether, or mixtures thereof to hydrocarbonsincluding olefins and aromatics with reaction conditions including atemperature of from about 275° C. to about 600° C., a pressure of fromabout 0.5 atmosphere to about 50 atmospheres and a liquid hourly spacevelocity of from about 0.1 to about 100.(V) The oligomerization of straight and branched chain olefins havingfrom about 2 to about 5 carbon atoms. The oligomers which are theproducts of the process are medium to heavy olefins which are useful forboth fuels, i.e., gasoline or a gasoline blending stock, and chemicals.The oligomerization process is generally carried out by contacting theolefin feedstock in a gaseous phase with a zeolite-bound high silicazeolite at a temperature in the range of from about 250° C. to about800° C., a LHSV of from about 0.2 to about 50 and a hydrocarbon partialpressure of from about 0.1 to about 50 atmospheres. Temperatures belowabout 250° C. may be used to oligomerize the feedstock when thefeedstock is in the liquid phase when contacting the zeolite-bound highsilica zeolite catalyst. Thus, when the olefin feedstock contacts thecatalyst in the liquid phase, temperatures of from about 10° C. to about250° C. can be used.(W) The conversion of C₂ unsaturated hydrocarbons (ethylene and/oracetylene) to aliphatic C₆₋₁₂ aldehydes and converting said aldehydes tothe corresponding C₆₋₁₂ alcohols, acids, or esters.(X) The desulfurization of FCC (fluid catalytic cracking) feed streams.The desulfurization process is generally carried out at a temperatureranging from 100° C. to about 600° C., preferably from about 200° C. toabout 500° C., and more preferably from about 260° C. to about 400° C.,at a pressure ranging from 0 to about 2000 psig, preferably from about60 to about 1000 psig, and more preferably from about 60 to about 500psig, at a LHSV ranging from 1 to 10 h⁻¹. The hydrocarbon mixtures whichcan be desulfurized according to the process of the present inventioncontain more than 150 ppm of sulfur, e.g., hydrocarbon mixtures with asulfur content higher than 1000 ppm, even higher than 10000 ppm.

The invention having been generally described, the following examplesare given as particular embodiments of the invention and to demonstratethe practice and advantages thereof. It is understood that the examplesare given by way of illustration and are not intended to limit thespecification or the claims to follow in any manner.

EXAMPLE 1 Synthesis of Sn—Ge-ZSM-5 Chemicals Used:

Tin (II) chloride dihydrate, SnCl₂*2H₂O, 98%; Sigma-Aldrich; Sodiumhydroxide solution, 50% in water; Sigma-Aldrich; Germanium oxide GeO₂,99.99%; Germanium Corporation of America, GTAH 68002;

Sodium aluminate (23.6% Al₂O₃; 19.4% Na₂O; 57.0% H₂O); Southern Ionics;

Ludox AS-40 colloidal silica, 40 wt. % suspension in water; Aldrich;

Tetrapropylammonium bromide TPABr, 98%; Alfa-Aesar; Acetic acid, 99.7%;Aldrich.

Solution #1. 2.21 grams of tin chloride dihydrate were dissolved in 55grams of D.I. water. 25.98 grams of sodium hydroxide solution were addedto the same solution with stirring. 1.0462 grams of GeO₂ were dissolvedin solution also.

Solution #2. 3.84 grams of sodium aluminate were homogenized in 50 gramsof D.I. water.

Solution #3. 28.12 grams of TPABr were dissolved in 100 grams of D.I.water.

Solution # 1 was added to 150 grams of Ludox AS-40 with gel formation.Stirring was made for 10 minutes. Then solution #2 was introduced togel. Gel was stirred for 15 minutes. Then solution #3 was added to geland stirring was continued for 60 minutes. 15.97 grams of acetic acidwere added gradually with gel stirring. Gel pH was measured in 30minutes after acid addition (pH=10.59).

Crystallization was made in 1 L stainless steel autoclave at 160° C. for4 days with stirring (200 rpm).

Material was washed and filtered with D.I. water, dried at 90° C.,sieved to 40 mesh size and calcined at 550° C. for 10 hours.

XRF analysis results are: 0.686 wt. % Na; 42.38 wt. % Si; 0.75 wt. % Al;1.52 wt. % Sn; 0.96 wt. % Ge.

Identified as ZSM-5 by XRD.

Synthesis of 1% Pt/CsGeSnZSM-5

3.8 grams of laboratory prepared SnGeZSM-5 was washed with 200 ml ofaqueous CsNO3 (0.5M) then filtered. The filtrate was then rewashed 3more times with 0.5M CsNO3 and rinsed with deionized H2O on the finalfiltering. The zeolite powder was then calcined for 3 hours at 280° C.in air.

Incipient wetness impregnation was carried out by adding drop wise asolution of 0.0432 g Pt(NH₂)₄(NO₃)₂ dissolved in 0.9327 g of deionizedwater to 2.047 grams of the Cs-exchanged SnGeZSM-5. The material wasdried for 1 hour in a 110° C. drying oven then calcined at 280° C. for 3hours. Elemental analysis gave 41.74 wt % Si, 0.73 wt % Al, 0.85 wt %Ge, 2.25 wt % Sn, 6.34 wt % Cs and 0.80 wt % Pt.

The catalyst powder was pressed and sized to 20-40 mesh. 0.25 cm³ (0.128g) of the sized catalyst was mixed with 1.75 ml of inert quartz chipsand was pretreated at 460° C. for 1 hour in flowing H2. Catalytictesting was then started.

EXAMPLE 2 Synthesis of Ge—B-ZSM-5 Chemicals Used:

Boric acid H₃BO3; 99.99%; Aldrich;

Sodium hydroxide NaOH; >98%; Aldrich;

Tetrapropylammonium bromide (CH₃(CH₂)₂)4NBr; 98%; Alfa-Aesar;

Germanium dioxide GeO₂;Germanium Corporation of America GTAH 68002;

Ludox HS-30 SiO₂, colloidal silica, 30% suspension in water;Sigma-Aldrich.

2.304 grams of sodium hydroxide were dissolved in 184 grams of D.I.water. 0.96 gram of boric acid and then 28.96 grams oftetrapropylammonium bromide were dissolved in the same solution withstirring. 1.2527 grams of germanium dioxide were dissolved graduallywith stirring. Gel was formed after 35.2 grams of Ludox HS-30 wereintroduced into solution. Gel was stirred for about 15 minutes(pH=12.76).

Crystallization was made in stainless steel 300 ml autoclave at 165° C.for 5 days with stirring (100 rpm).

Analysis results are: 41.6 wt. % Si; 0.41 wt. % B; 0.83 wt. % Ge.Identified as ZSM-5 by XRD.

Synthesis of 1% Pt/CsBGeZSM-5

2.4 grams of laboratory prepared BGeZSM-5 was washed with 150 ml ofaqueous CsNO₃ (0.5M) then filtered. The filtrate was then rewashed 3more times with 0.5M CsNO₃ and rinsed with deionized H₂O on the finalfiltering. The zeolite powder was then calcined for 3 hours at 280° C.in air.

Incipient wetness impregnation was carried out by adding drop wise asolution of 0.0310 g Pt(NH₂)₄(NO3)₂ dissolved in 0.7637 g of deionizedwater to 1.509 grams of the Cs-exchanged BGeZSM-5. The material wasdried for 1 hour in a 110° C. drying oven then calcined at 280° C. for 3hours. Elemental analysis gave 42.85 wt % Si, 0.63 wt % Ge, 0.256 wt %B, 6.24 wt % Cs, and 0.74 wt % Pt.

The catalyst powder was pressed and sized to 20-40 mesh. 0.25 cm3 (0.130g) of the sized catalyst was mixed with 1.75 ml of inert quartz chipsand was pretreated at 460° C. for 1 hour in flowing H2. Catalytictesting was then started.

EXAMPLE 3 Synthesis of B-ZSM-5 Chemicals Used:

Boric acid H₃BO₃; 99.99%; Aldrich;

Sodium hydroxide NaOH; >98%; Aldrich;

Tetrapropylammonium bromide (CH₃(CH₂)₂)₄NBr; 98%; Alfa-Aesar;

Ludox HS-30 SiO₂, colloidal silica, 30% suspension in water;Sigma-Aldrich.

2.88 grams of sodium hydroxide were dissolved in 230 grams of D.I.water. Then 1.2 grams of boric acid and then 36.20 grams oftetrapropylammonium bromide were dissolved in the same solution withstirring. Light gel was formed after 44.0 grams of silica source LudoxHS-30 were introduced.

Crystallization was made in a one liter stainless steel autoclave at165° C. for 5 days with stirring (100 rpm).

Analysis results are: 42.7 wt. % Si; 0.411 wt. % B. Identified as ZSM-5by XRD.

Synthesis of 1% Pt/BZSM-5

Incipient wetness impregnation was carried out by adding drop wise asolution of 0.0402 g Pt(NH₂)₄(NO₃)₂ dissolved in 0.9925 g of deionizedwater to 2.011 grams of laboratory prepared BZSM-5. The material wasdried for 1 hour in a 110° C. drying oven then calcined at 280° C. for 3hours. Elemental analysis gave 44.99 wt % Si, 0.682 wt % Na, and 0.94 wt% Pt. Boron content was not measured.

The catalyst powder was pressed and sized to 20-40 mesh. 0.25 cm³ (0.128g) of the sized catalyst was mixed with 1.75 ml of inert quartz chipsand was pretreated at 460° C. for 1 hour in flowing H2. Catalytictesting was then started.

EXAMPLE 4 Synthesis of 1% Pt/CsBZSM-5

2.7 grams of laboratory prepared BZSM-5 was washed with 150 ml ofaqueous CsNO₃ (0.5M) then filtered. The filtrate was then rewashed 3more times with 0.5M CsNO₃ and rinsed with deionized H2O on the finalfiltering. The zeolite powder was then calcined for 3 hours at 280° C.in air.

Incipient wetness impregnation was carried out by adding drop wise asolution of 0.0402 g Pt(NH₂)₄(NO₃)₂ dissolved in 0.9925 g of deionizedwater to 2.019 grams of the Cs-exchanged BZSM-5. The material was driedfor 1 hour in a 110° C. drying oven then calcined at 280° C. for 3hours. Elemental analysis gave 44.06 wt % Si, 0.234 wt % B, 5.74 wt %Cs, and 0.86 wt % Pt.

The catalyst powder was pressed and sized to 20-40 mesh. 0.25 cm³ (0.124g) of the sized catalyst was mixed with 1.75 ml of inert quartz chipsand was pretreated at 460° C. for 1 hour in flowing H2. Catalytictesting was then started.

EXAMPLE 5 Synthesis of B-Al-ZSM-5 Chemicals Used:

Boric acid H₃BO3; 99.99%; Aldrich;

Sodium hydroxide NaOH; >98%; Aldrich;

Sodium aluminate NaAlO₂ (23.6 wt. % Al₂O₃; 19.4 wt. % Na₂O; 57 wt. %H₂O); Southern Ionics.

Tetrapropylammonium bromide (CH₃(CH₂)₂)₄NBr; 98%; Alfa-Aesar;

Ludox HS-30 SiO₂, colloidal silica, 30% suspension in water;

Sigma-Aldrich.

3.7939 grams of sodium hydroxide were dissolved in 345 grams of D.I.water. 1.8 grams of boric acid were dissolved in the same solution. Thensodium aluminate (1.3582 grams) was added and then 54.3 grams oftetrapropylammonium bromide were dissolved in the same solution withstirring. Silica source Ludox HS-30 (66.0 grams) was introduced into thesolution with gel formation. Gel was stirred for 10-15 minutes(pH=13.03).

Crystallization was made in 1 L stainless steel autoclave at 165° C. for5 days with stirring (100 rpm).

Analysis results are: 37.5 wt. % Si; 0.248 wt. % B; 0.97 wt. % Al.

Identified as ZSM-5 by XRD.

Synthesis of 1% Pt/CsBZSM-5

2.7 grams of laboratory prepared BZSM-5 was washed with 150 ml ofaqueous CsNO3 (0.5M) then filtered. The filtrate was then rewashed 3more times with 0.5M CsNO₃ and rinsed with deionized H2O on the finalfiltering. The zeolite powder was then calcined for 3 hours at 280° C.in air.

Incipient wetness impregnation was carried out by adding drop wise asolution of 0.0409 g Pt(NH₂)₄(NO₃)₂ dissolved in 0.9257 g of deionizedwater to 2.054 grams of the Cs-exchanged BZSM-5. The material was driedfor 1 hour in a 110° C. drying oven then calcined at 280° C. for 3hours. Elemental analysis gave 42.11 wt % Si, 0.126 wt % Al, 0.90 wt %B, 9.13 wt % Cs, and 0.68 wt %.

The catalyst powder was pressed and sized to 20-40 mesh. 0.25 cm3 (0.127g) of the sized catalyst was mixed with 1.75 ml of inert quartz chipsand was pretreated at 460° C. for 1 hour in flowing H2. Catalytictesting was then started.

EXAMPLE 6 Synthesis of Ge—B-ZSM-5 Chemicals Used:

Boric acid H₃BO3; 99.99%; Aldrich;

Sodium hydroxide NaOH; >98%; Aldrich;

Tetrapropylammonium bromide (CH₃(CH₂)₂) 4NBr; 98%; Alfa-Aesar;

Germanium dioxide GeO2; Germanium Corporation of America GTAH 68002;

Ludox HS-30 SiO₂, colloidal silica, 30% suspension in water;Sigma-Aldrich.

2.304 grams of sodium hydroxide were dissolved in 184 grams of D.I.water. 0.96 gram of boric acid and then 28.96 grams oftetrapropylammonium bromide were dissolved in the same solution withstirring. 1.2527 grams of germanium dioxide were dissolved graduallywith stirring. Gel was formed after 35.2 grams of Ludox HS-30 wereintroduced into solution. Gel was stirred for about 15 minutes(pH=12.76).

Crystallization was made in stainless steel 300 ml autoclave at 165° C.for 5 days with stirring (100 rpm).

Analysis results are: 41.6 wt. % Si; 0.41 wt. % B; 0.83 wt. % Ge.Identified as ZSM-5 by XRD.

1% Pt/GeBZSM-5

Incipient wetness impregnation was carried out by adding drop wise asolution of 0.0412 g Pt(NH₂)₄(NO₃)₂ dissolved in 0.96 grams of deionizedwater to 2.003 grams of laboratory prepared GeBZSM-5. The material wasdried for 1 hour in a 110° C. drying oven then calcined in air at 280°C. for 3 hours.

The catalyst powder was pressed and sized to 20-40 mesh. 0.25 cm3 (0.127g) of the sized catalyst was mixed with 1.75 ml of inert quartz chipsand was pretreated at 460° C. for 1 hour in flowing H₂. Catalytictesting was then started.

Catalyst Testing

All catalysts were tested according to the same procedure. Catalystparticles, mixed with inert quartz chips, were loaded into a ¼″ OD plugflow reactor. n-hexane was vaporized into a stream of flowing hydrogenat a temperature of approximately 150° C. This gas mixture was passedthrough the reactor at a LHSV of 8.6 hr⁻¹, the reactor being maintainedat a temperature of 515° C. by an external heating jacket. The reactionproducts were analyzed by gas chromatography. Products ranging in sizefrom methane to dimethylnaphthalene were observed. A variety of C6isomerization products were observed, including isohexanes (e.g.,2-methylpentane) and olefins (e.g. 1-hexene.) For the purposes ofcalculating conversion and selectivity, these C₆ products wereconsidered to be unreacted. The selectivities reported are calculated asthe sum of benzene, toluene, xylenes, and ethylbenzene produced dividedby the total amount of all benzene, C1-C5, and C7+ materials recovered.These selectivities are presented on a molar C6 basis.

Sn, Ge, B in final Example catalyst Si/Al₂ catalyst X₂₅ S₂₅ 1Pt/CsSnGeZSM-5 110  2.3% Sn, 11 86 0.85% Ge 2 Pt/CsBGeZSM-5 ∞ 0.29% B,35 75 0.63% Ge 3 Pt/BZSM-5 ∞ 0.41% B 43 78 4 Pt/CsBZSM-5 ∞ 0.25% B 51 875 Pt/CsBZSM-5  90 0.14% B 45 72 6 Pt/BGeZSM-5 ∞ 0.41% B, 24 91 0.63% Ge

Numerous modifications and variations of the present invention arepossible in light of the above teachings. It is to be understood that,within the scope of the appended claims, the invention may be practicedother than as specifically described.

1. A catalyst for conversion of hydrocarbons comprising: a) a zeolitehaving germanium and at least one element selected from the groupconsisting of tin and boron incorporated into the zeolite framework andb) at least one metal selected from Group 10 deposited on the zeolite.2. The catalyst of claim 1 wherein the metal deposited on the zeolite isplatinum.
 3. The catalyst of claim 1 wherein the zeolite is MFI (ZSM-5).4. The catalyst of claim 1 wherein the zeolite is non-acidic.
 5. Aprocess for synthesizing a zeolite comprising: a) preparing a zeolitehaving germanium and at least one selected from the group consisting oftin and boron incorporated into the zeolite framework; b) depositing atleast one metal selected from Group 10 on the zeolite; and c) calciningthe zeolite, said calcining occurring after preparation of the zeolite,before depositing at least one metal selected from Group 10 on thezeolite or after depositing at least one metal selected from Group 10 onthe zeolite.
 6. The process of claim 5 wherein the metal deposited onthe zeolite is platinum.
 7. The process of claim 5 wherein the zeoliteis MFI (ZSM-5).
 8. The process of claim 5 wherein the zeolite isbase-exchanged with an alkali metal or alkaline earth metal to make thezeolite non-acidic.
 9. A process for the conversion of hydrocarbonscomprising: a) contacting a hydrocarbon stream containing alkanes,olefin or mixtures thereof having 2 to 12 carbon atoms per molecule withat least one zeolite-based catalyst wherein the catalyst containsgermanium and at least one selected from the group consisting of tin andboron incorporated into the zeolite framework and wherein at least onemetal selected from Group 10 has been deposited on the zeolite; and b)recovering the product.
 10. The process of claim 9 wherein the metaldeposited on the zeolite is platinum.
 11. The process of claim 9 whereinthe zeolite is MFI (ZSM-5).
 12. The process of claim 9 wherein thezeolite is non-acidic.
 13. The process of claim 9 wherein the alkanes orthe olefins are straight, branched, cyclic or mixtures thereof.
 14. Acatalyst for conversion of hydrocarbons comprising: a) a zeolite havingboron incorporated into the zeolite framework and b) at least one metalselected from Group 10 deposited on the zeolite.
 15. The catalyst ofclaim 14 wherein the metal deposited on the zeolite is platinum.
 16. Thecatalyst of claim 14 wherein the zeolite is MFI (ZSM-5).
 17. Thecatalyst of claim 14 wherein the zeolite is aluminum-free.
 18. Thecatalyst of claim 14 wherein the zeolite is base-exchanged with analkali metal or alkaline earth metal to make the zeolite non-acidic. 19.A process for synthesizing a zeolite comprising: a) preparing a zeolitehaving boron incorporated into the zeolite framework; b) depositing atleast one metal selected from Group 10 on the zeolite; and c) calciningthe zeolite after preparation of the zeolite, before depositing at leastone metal selected from Group 10 on the zeolite or after depositing atleast one metal selected from Group 10 on the zeolite.
 20. The processof claim 19 wherein the metal deposited on the zeolite is platinum. 21.The process of claim 19 wherein the zeolite is MFI (ZSM-5).
 22. Theprocess of claim 21 wherein the zeolite is aluminum-free.
 23. Theprocess of claim 19 wherein the zeolite is base-exchanged with an alkalimetal or alkaline earth metal to make the zeolite non-acidic.
 24. Aprocess for the conversion of hydrocarbons comprising: a) contacting ahydrocarbon stream containing alkanes, olefins or mixtures thereofhaving 2 to 12 carbon atoms per molecule with at least one zeolite-basedcatalyst wherein the catalyst contains boron incorporated into thezeolite framework and wherein at least one metal selected from Group 10has been deposited on the zeolite; and b) recovering the product. 25.The process of claim 24 wherein the metal deposited on the zeolite isplatinum.
 26. The process of claim 24 wherein the zeolite is MFI(ZSM-5).
 27. The process of claim 24 wherein the zeolite isaluminum-free.
 28. The process of claim 24 wherein the alkanes or theolefins are straight, branched, cyclic, or mixtures thereof.
 29. Theprocess of claim 24 wherein the zeolite is base-exchanged with an alkalimetal or alkaline earth metal to make the zeolite non-acidic.
 30. Azeolite comprising: a ZSM-5 zeolite having germanium and at least oneselected from the group consisting of tin and boron incorporated intothe zeolite framework.
 31. A process for synthesizing a zeolitecomprising: a) preparing a ZSM-5 zeolite containing germanium and atleast one selected from the group consisting of tin and boronincorporated into the zeolite framework; b) calcining the zeolite.